WO2012150186A1

WO2012150186A1 - Filtration membrane

Info

Publication number: WO2012150186A1
Application number: PCT/EP2012/057739
Authority: WO
Inventors: Allan HJARBÆK HOLM
Original assignee: Grundfos Management AS
Current assignee: Grundfos Management AS
Priority date: 2011-05-04
Filing date: 2012-04-27
Publication date: 2012-11-08
Anticipated expiration: 2013-11-04
Also published as: EP2520355A1; US9393528B2; EP2520355B1; US20140048487A1

Abstract

A filtration membrane (4) comprising a porous base layer (8) arranged adjacent to a filtration layer (6) having pores (10) extending through the filtration layer (6). The filtration layer is electrically conductive and that at least one compound (24, 26) is attached on the filtration layer (6) and hereby providing a protective surface layer (40). The at least one compound (24, 26) is configured to be at least partially cleaved off the filtration layer (6) by a predefined cleave off process.

Description

Title: Filtration membrane

Description

The invention generally relates to a filtration membrane. The invention more particularly generally relates to filtration membrane intended for filtration of fluids in which the occurrence of fouling represents a significant problem/challenge.

Membranes are used in a wide variety of separation applications including food and beverage and water treatment industries. By nature the membrane, the surface contains pores onto which organics, bacteria, and microbes can readily settle, particularly when there is an ap- plied pressure on the system to increase water flux across the membrane.

Depending on the specific system a wide variety of membrane fouling can occur; scaling due to concentration polarization, bio-fouling due to adhesion of bacteria and growth of biofilms, colloidal fouling from suspended particles, organic films from natural organic matter and humic acids by way of example.

In some applications repetitive use of back flush is not sufficient to keep the membrane clean and thus a cleaning process (CIP), in which cleaning chemicals are used, is required. In heavy fouling fluids it would be an advantage to have a filtration membrane having intrinsic anti fouling properties. The object of the invention is to provide a filtration membrane that is easy to use and clean when applied in heavy fouling fluids. I† is an object of the invention to provide a filtration membrane that is suitable of being used in applications in which back flush is not sufficient to clean the membrane.

These objects can be achieved by a filtration membrane having the features defined in claim 1 . Preferred embodiments are defined in the dependant sub claims and explained in the following description and shown in the accompanying drawings.

The filtration membrane according to the invention comprises a porous base layer attached to an electrically conductive filtration layer having pores extending through the filtration layer. At least one compound is attached on the filtration layer and hereby providing a protective sur- face layer. The at least one compound is configured to be at least partially cleaved off the filtration layer by a predefined cleave off process.

The electrically conductive filtration layer may have an electrical con- ductivity exceeding 1000 S m-1 at 293 K.

The protective surface layer inhibits a fouling layer from growing on the filtration layer. The fouling layer is prevented from growing directly at the surface of the filtration layer. Fouling can grow on the protective surface layer and this fouling can be removed by cleaving off the at least one compound from the filtration layer. Thus, the filtration membrane is easy to use and clean when applied in heavy fouling fluids. Besides the filtration membrane is suitable of being used in applications in which back flush is not sufficient to clean the membrane.

It may be an advantage that the at least one compound is configured to be attached on the filtration layer and to be at least partially cleaved off fhe profecfive surface layer filfrafion layer by a reversible elecfrochemical process.

An elecfrochemical process may used†o provide a very accurate con- trol of fhe attachment of fhe protective surface layer. When a reversible elecfrochemical process is applied it is possible†o build fhe protective layer and to af least partially cleave the protective layer off by using elecfrochemical regulation means. A reversible elecfrochemical process may carried out by using a two electrode system (a work electrode and a counter electrode) or a three electrode system (a work electrode, a counter electrode and a reference electrode) to provide an electric field af the filter membrane surface and hereby influence and control the elecfrochemical proc- esses in region at and close†o the surface of fhe filtration membrane.

It is possible†o attach a compound on the filtration layer by using a heat source†o heaf up the part of fhe filtration layer on to which fhe at least one compound is intended†o be attached. It is also possible†o af least partially cleave off a compound from fhe filtration layer by heating up areas of fhe filtration membrane.

Preferable fhe heat up process is carried ouf locally at fhe filtration surface. In this way the intended chemical reactions will occur only af the areas that are heated up.

It may beneficial that fhe at least one compound is a diazonium salt:

R-N2⁺ X^" , where R is aryl and where X is an inorganic or organic anion.

Diazonium salts are capable of generating a very reactive compound that can be attached on the filtration layer. When an electron is transferred to a diazonium salts a highly reactive compound is created and this compound can attach to the filtration layer and hereby start building up a protective surface layer at the filtration layer if the reactive compound is situated close to the surface of the filtration layer.

Preferable the diazonium compound is on the following form:

R-N2⁺ X^" , where R is aryl and where X is an inorganic anion

This type of diazonium salts are suitable of being used to build up a protective surface layer at the filtration layer surface.

It may be an advantage that the filtration membrane is configured in a manner so that the thickness of the protective surface layers can be controlled by using an electrochemical process. The protective surface layer may comprise one or more layers of at least one compound. It is possible to use compounds containing polyethylene glycol (PEG) chains of various chain lengths and hereby provide either a thin protective surface layer or a thicker protective surface layer.

Hereby effect of various thickness of the grafted layer can be achieved. It would be possible to provide the best anti-fouling property depending on the fluid and the properties of the filtration membrane. It may be an advantage to use an electrochemical process to control the thickness and/or porosity of the protective surface layer because an electrochemical process can be used to exercise at least partial regulation of the layer thickness. This will be known to a person skilled in the art. An electrochemical process may be applied to deliver electrons to the diazonium salts in a certain distance from the surface of the filtration layer. When a high voltage (potential) is applied at the filtration layer surface a protective layer generating chemical reaction can be initiated in a comparatively large distance from the surface of the filtration layer. However, in a situation where a low voltage (potential) is applied at the filtration layer surface a protective layer generating chemical reaction can be initiated in a shorter distance from the surface of the filtration layer.

It may be an advantage to use a diazonium salt of the following form:

The diazonium salt in a), 4-(carboxyl) phenyl diazonium tetrafluorobo- rate, is easily synthesized using protocols well known to a person skilled in the art from a pertinent precursor (p-amino-benzoic acid). It may be advantageous to use this particular diazonium compound due to its hydrophilic character as well as its ability to be deproto- nated/protonated as a function of pH, i.e. reversibly tune its hydrophilic and charge character. This characteristic may be advantageous in media in which an increase of the hydrophilic character of the membrane reduces the propensity of membrane fouling. In addition, it is known that charged layers on membranes have a tendency to reduce fouling. The diazonium salt in b), 4-(me†hoxy) phenyl diazonium tetrafluorobo- ra†e, is easily synthesized using protocols well known to a person skilled in the art from a pertinent precursor (p-me†hoxy aniline). Another related promising compound is provided by the commercially available Fast Blue BB salt. It may be advantageous to use these particular diazonium salts as they provide a simplified system incorporating the ether linkage between the benzene ring and substituent. This in part increases the hydrophilic character of the film formed at the surface. Due to the strong electron donating nature of this substitution pattern, such protec- tive layers are comparatively easy to oxidise (i.e. cleave off the surface).

The diazonium salt in c), 4-(2-(2-(me†hoxy)e†hoxy)e†hoxy) phenyl diazonium tetrafluoroborate, may offer significant advantages due to the incorporation of a polyethylene glycol function in the layer. It has been shown that polyethylene glycol functionalities in membranes make the membranes much less prone to fouling. In particular this functionality is known to reduce the so-called adsorptive fouling in which a first layer of water molecules is replaced by the fouling solute. The reduction of ad- sorptive fouling is mainly due to the hydrophilic character of the polyethylene glycol functionality. This may be advantageous in media in which increasing the hydrophilic character of the membrane reduces the propensity of membrane fouling. The forth example d), 4-(ni†ro) phenyl diazonium tetrafluoroborate, is a well known salt to a person skilled in the art. The advantage of this particular salt is that its hydrophilic character may be varied by controlling the oxidation state of the appended nitrogen atom. In the highest oxidation state, NO2, it is somewhat polar but can easily (by electro- chemical means) be transformed into the reduced forms such as hy- droxyl amine, -NHOH, or amine, -NH2. These latter functional groups can be deprotonated/protonated by change in the pH of the medium and thus, they also have the option to exercise controlled hydrophilic character. Moreover, by reduction of the nitro group to hydroxyl amine or amine, the electronic properties of the nitrogen can be tuned. The nitro group is a strong electron withdrawing group, whereas the amine func- tionality is an electron donating group with the hydroxylamine placed in between. Tuning of the electronic properties of the functional group provides a means for change in the surface properties of the filtration layer. Furthermore, if either 4-(hydroxylamine) phenyl diazonium tetra- fluoroborate or 4-(amino) phenyl diazonium tetrafluoroborate are at- tached to the filtration layer surface the nitrogen based functional groups provide a tag for further chemical modifications of the surface which are not possible with the nitro group.

It may be an advantage that the filtration layer is a metal layer. Since a metal layer is electrically conductive it is possible to connect the filtration layer to an electrical source and hereby use the filtration layer as a working electrode. Thus, a compound can be attached on the filtration layer and hereby providing a protective surface layer by simple means. The at least one compound can be at least partially cleaved off the filtration layer by changing the voltage applied to the surface of the filtration layer.

It is also possible to have a filtration layer made in another electrically conductive material such as electrically conductive composite, carbon or another suitable material.

It may be an advantage that the filtration layer is made of stainless steel. Stainless steel has several advantageous properties that make it suitable for being used as filtration layer in a filtration membrane ac- cording to the invention. It is possible to provide a corrosion resistant stainless steel filtration layer having pores in the desired size range e.g. by a sintering process. I† may be an advantage†o have a filtration membrane in which the porous base layer and the filtration layer are made of the same material. It may beneficial the porous base layer and the filtration layer are made in stainless steel.

It may be beneficial that the pore size in the filtration layer lies within the range between 10 nm and 500 nm, preferable between 10 nm and 200 nm. A filtration membrane having a filtration layer with pores within these ranges can be applied to filter fluids in the desired filtration range. It is possible to have a filtration layer with huge, moderate or low pore size deviation. In some applications it may be an advantage that the filtration layer has pores in a large size range. In other applications it may be an advantage that the pores in the filtration layer have basi- cally equal size.

It may be beneficial that the pore size in the porous base layer lies within the range between 100 nm to 100 μιτι, preferable 0.5-10 μιτι. Hereby it is achieved that the filtered fluid easily can be transported through porous base layer. A porous base layer having pores in this range can be provided with the required mechanical strength so that it is suitable for being a base for the filtration layer.

Advantageously, the thickness d of the filtration layer is 50 nm-10 μιτι, preferable 200 nm-1000 nm. Hereby it is achieved that an optimum filtration can be carried out by the filtration layer and that the filtration layer has the required mechanical strength and is sufficiently thin to provide an optimum flux through the filtration layer. It may be beneficial that the thickness d of the porous base layer is 300- 3000 μιτι, preferable 500-1500 μιτι. Hereby the porous base is provided with the required mechanical strength and thus it is suitable for being a base for the filtration layer.

It is possible to use the filtration membrane in a filtration system. The fil- tration system may be any suitable type of filtration system. Such system may be a very simple and require manual process. An alternative system may be fully or partially automated. It may be an advantage to apply the filtration membrane in a filtration system that is adapted to the specific application.

Advantageously a filter membrane according to one of the claim 1 -12 is used to filter the fluid. Such method makes it possible to carry out filtration of heavy fouling fluids in applications in which back flush is not sufficient to clean the membrane.

It may be an advantage that the filtration membrane is plate shaped and has a rectangular geometry. It is possible to have a filtration membrane that consists of several filtration membranes put together to one larger filtration membrane.

The present invention will become more fully understood from the detailed description given herein below and the accompanying drawings are given by way of illustration only, and thus, they are not limitative of the present invention, and wherein:

Fig. 1 shows a schematical cross-sectional view of a filtration layer of a filtration membrane according to the invention; shows a schematic cross-sectional view of a filtration layer of a filtration membrane according to the invention; shows a close up view of a filfrofion layer provided with a protective surface layer; shows a close up view of a filtration layer during a filtration process; shows a close up view of a filtration layer after the protective surface layer has been removed from if; shows a schematic cross-sectional view of a filtration system according†o the invention; shows a close up view of a filtration layer before attachment of a compound†o the filtration layer surface; shows a close up view of fhe filtration layer shown in Fig. 5 a when the compound is attached to fhe filtration layer surface; shows a close up view of a filtration layer according to fhe invention; shows a close up view of a filtration layer in a situation where the surface layer is being cleaved off fhe filtration layer; shows a close up view of a grafted layer where the compounds are having long chain lengths; Fig. 7 b shows a close up view of a grafted layer where the

pounds are having shorter chain lengths; is a graph showing the flux ratio versus time for a prior art filtration membrane and a filtration membrane according to the invention; Fig. 8 b is a graph showing the flux ratio versus time before and after a CIP process for a prior art filtration membrane and a filtration membrane according to the invention; shows examples of compounds that can be used to build an anti fouling layer on a filtration layer of a filtration membrane; shows example of a compound reaction leading to deposition of an anti fouling layer on a filtration layer of a filtration membrane and shows how additional layers can be added to the layer shown in Fig. 9. Other objects and further scope of applicability of the present invention will become apparent from the detailed description given hereinafter. It should be understood, however, that the detailed description and specific examples and indications of preferred embodiments of the invention, are given by way of illustration only, since various changes and modifications within the spirit and scope of the invention will be apparent to those skilled in the art from this detailed description.

Referring now in detail to the drawings for the purpose of illustrating preferred embodiments of the present invention, elements of a filtration membrane 4 according to the present invention is illustrated in Fig. 1 -3. The filtration membrane 4 comprises a porous base layer 8 and a filtration layer 6. The filtration layer 6 is attached to the base layer 8 and the filtration layer 6 is provided with pores 10 extending through the filtration layer 6. The pores 10 of the filtration layer 6 may preferable be configured to filter foulants or particles within a specific size range since filtration of small foulants and small particles generally requires smaller pores than filtration of larger particles and foulants.

Fig. 1 shows that the thickness d of the filtration layer 6 is much smaller than the thickness D of the base layer 8. A compound is attached on the filtration layer 6 so that the attached compound constitutes a pro- tective surface layer 40. The protective surface layer is configured to be at least partially cleaved off the filtration layer 6. Moreover, the filtration layer 6 is configured in a way so that a compound can be attached on the filtration layer 6 after the protective layer has been completely or partially cleaved off the filtration layer 6. This may be done by using various methods.

It may be an advantage that the base layer 8 is made in a porous material on to which it is easy to attach the filtration layer 6. It may be an advantage if the base layer 8 and the filtration layer are made in the same materials. By way of example it is possible to make the base layer 8 and the filtration layer in stainless steel. However, it is possible to apply any other suitable material. It is possible to apply ceramic materials, composites, metals or another suitable material. It is possible to make the base layer 8 and the filtration layer 6 in two different materials. A person skilled in the art would be able to join the base layer 8 and the filtration layer 6 even if they are made in different materials.

The filtration membrane 4 may have any suitable geometry. By way of example the filtration membrane 4 may be plate shaped. It is possible to have a filtration membrane 4 that has a curved geometry of a plane geometry. It is possible to build a large filtration membrane 4 out of several smaller filtration membranes 4 that are put together to constitute a large filtration membrane 4.

Fig. 2 a) illustrates a close up view of a filtration membrane 4 having a filtration layer 6 with a number of pores 1 0. The width Wi of the pores 10 of the filtration layer 6 are indicated in Fig. 2 and it can be seen that the width Wi of the pores 1 0 vary. It may be assumed that the width Wi of the pores 1 0 follow a Gaussian distribution. Fig. 2 b) illustrates a close up view of a filtration layer 6 of a filtration membrane 4 according to the invention. The filtration layer 6 is provided with a protective surface layer 40. The protective surface layer 40 is thinner than half of the width Wi of the pores 10 of the filtration layer 6. The width Wi of the pores 10 of the filtration layer 6 vary slightly. The filtration layer 6 is provided with a surface layer 40 that covers the surface of the filtration layer 6. Accordingly, the whole surface of the filtration layer 6 is protected by the surface layer 40.

The thickness of the protective surface layer 40 may vary. It is possible to have a filtration layer 6 with a thickness of 1 -500 nm by way of example. The width W2 of the free space in the pores 10, after the protective surface layer 40 has been deposited on the filtration layer 6, is significantly smaller than the width Wi of the free space in the pores 1 0 before the protective surface layer 40 deposition has occurred. Therefore, the deposition of the protective surface layer 40 affects the filter characteristics of the filter membrane 4. The width Wi of the free space in the pores 1 0, before the surface layer 40 has been attached to the filtration layer 6, may be in the range of 1 0-500 nm by way of example and the width W2 of the free space in the pores 10, after a surface layer 40 has been deposited on the filtration layer 6, may be decreased by 2-50% by way of example. I† is, as an example, possible†o have a filtration membrane 4 in which the width Wi of fhe free space in fhe pores 10, before fhe surface layer 40 has been attached to fhe filtration layer 6, is 100 nm and where the widfh W2 of fhe free space in fhe pores 10 offer a surface layer 40 has been deposited on the filtration layer 6 is 50 nm.

Fig. 3 a) illustrates a close up view of a filtration layer 6 of a filtration membrane 4 during a filtration process. During the filtration process the fluid 14 that is being filtered by a membrane filter 4 according to fhe invention is being guided along the surface of fhe filtration layer 6 of fhe filtration membrane 4. When a filtration membrane 4 according to fhe present invention is used in a cross flow filtration setup a mean stream of fhe fluid 14 may travel along an axis, X, that is parallel to fhe surface of fhe filtration layer 6. A portion of fhe fluid 14 enters the pores 10 of fhe filtration layer 6 and this portion of fhe fluid 14 is moving along fhe axis, Y, perpendicular fo fhe surface of fhe filtration layer 6. It can be seen from Fig. 3 a) that foulanfs 42, 43, 44 are present in the fluid 14 and that some of these foulanfs 42, 43, 44 settle along the surface of fhe pores 10. This phenomenon is known as fouling. Settlement of fou- lanfs 42, 43, 44 will increase fhe resistance for fluid passage through the pores 10. Accordingly, fhe flux across fhe filtration membrane 4 (especially the flux through the filtration layer 6 of fhe filtration membrane 4) will decrease unless a higher pressure is applied to force fluid through the filtration membrane 4.

Fig. 3 a) shows that the fouling occurs in a distance from fhe filtration layer 6 because the protective surface layer 40 is protecting the filtration layer 6. In Fig. 3 b) the protective surface layer 40 has been removed by a "cleave off process" (this may be done by using electrochemical means). Even though most of fhe foulanfs 42, 44 have been removed from the filtration layer 6, a few foulants 42, 44 are still attached to the filtration layer 6. However, since the filtration layer 6 is almost free of foulants 42, 43, 44 the filtration layer 6 is suitable for being used to filter a fluid 14. Preferably, a new protective surface layer 40 is provided to the filtration layer 6 before the filtration layer 6 is used to filter the fluid 14. The foulants 42, 43, 44 may in principle be any type of foulants such as bacteria or inorganic particles by way of example.

In some applications it may be possible to cleave off all foulants 42, 43, 44 from the filtration layer 6. A new protective surface layer 40 may preferable be grafted on the filtration layer 6 before the filtration layer 6 is being reused to filter a fluid 14.

Fig. 4 illustrates a schematic cross-sectional view of a filtration system 2 using a filtration membrane 4 according to the invention. The filtration system 2 comprises a housing 22 configured to guide a fluid 14 along a filtration membrane 4. The housing 22 comprises a fluid inlet 16 through which the fluid 14 enters the housing 22. The housing 22 moreover comprises a fluid outlet 18 for guiding away the fluid 14 that has passed the filtration membrane 4. The fluid 14 that is drained through the fluid outlet 18 may be circulated to the fluid inlet 1 6 through a fluid pipeline (not shown).

The housing 22 comprises a base member 46, and a top member 50. Together these members 46, 50 constitute a space 52 configured to receive and guide the fluid 14 from the fluid inlet 16 along the surface of the filtration membrane 4 and through the fluid outlet 18.

That portion of the fluid that 14 enters the filtration membrane 4 will ini- tially pdss through the surfoce of the filtration layer 6 (see Fig. 1 ) that will retain items in the liquid that are larger than the pore size of the membrane. Hereafter the filtered fluid (permeate) will continue through the base layer 8 and eventually be drained through the permeate outlet 20. The travel direction of the fluid is indicated with arrows.

A seal ring 34 are provided between the filtration membrane 4 and the distal ends of the filtration membrane 4 and the side members 46, 48 and the top member 50. An electrical source 12 is arranged next to the filtration system 2. This electrical source 12 delivers the voltage that is applied to the working electrode 28, the counter electrode 30 and the reference electrode 32. The working electrode 28 is connected to the electrical source 12 by a wire 54. The counter electrode 30 is connected to the electrical source 12 by a wire 56 and the reference electrode 32 is connected to the electrical source 12 by a wire 58. The electrical source 12 may comprise or be connected to a control unit (not shown) that is configured to regulate the potential at the working elec- trode 28, the counter electrode 30 and the reference electrode 32. The control unit may ne configured to regulate the potential at the electrodes 28, 30, 32 on the basis of external inputs (sensor inputs by way of example). When a suitable potential is provided to the surface of the filtration membrane 4 the surface of the filtration membrane 4 is capable of delivering electrons to compounds in the surrounding fluid 14. Hereby it is possible to initiate an electrochemical process. Under some conditions it is possible to reduce a compound 24, 26 when a positive electrical potential (relative to the counter electrode 30) is applied on the surface of the filtration membrane 6. Under other conditions reduction of a compound 24, 26 requires that a negative potential is applied on the surface of the filtration membrane 6. When a diazonium salt is present in the fluid 14 and the required conditions are present near the surface of the filtration membrane 4 it would be possible to reduce a diazonium salt 24, 26 that is present in the fluid 14. The diazonium salt can be reduced when a chemical driving force is present so that the will receive an electron and hereby cleave to release nitrogenous gas (N2) and generate a highly reactive radical, R, that preferably connects to the surface of the filtration membrane 4 by the creation of a covalent bond (see Fig. 9 b)). Under some conditions it is possible to reverse the electrochemical process and hereby at least partly cleave off the grafted protective surface layer 40 of the filtration layer 6 of the filtration membrane 4, by changing the electrochemical potential and/or polarity of the working electrode 28 and the counter electrode 30. Under some conditions, only very small changes in the potential of the filtration layer 6 of the filtration membrane 4 are required to initiate grafting of a protective surface layer 40 and/or to completely of partially cleave off a protective surface layer 40. Under some conditions even a positive potential (measured relative to the counter electrode) at the filtration membrane 4 can initiate grafting of a protective surface layer 40.

It is possible to use a direct current or an alternating current to control the build up of a protective surface layer 40 and the "cleave off proc- ess". Electrical pulsations may be used to provide the intended polarisation of the filtration membrane 4 via the working electrode 28. It is possible to use sensor signals to regulate when a protective surface layer 40 has to be grafted and when a protective surface layer 40 has to be cleaved off. A useful sensor signal may be the flux through the filtration membrane 4 or the transmembrane pressure (TMP).

Advantageously, the protective layer 40 is cleaved off during a back flush process. Hereby it is possible to make a very efficient cleaning of the filtration membrane 4. The protective layer 40 prevents fouling from growing directly on the surface of the filtration membrane 4. Instead the fouling grows on the protective surface layer 40. Accordingly, most of fhe fouling will be removed from fhe filfrofion membrane 4 when fhe profecfive surface layer 40 is cleaved off fhe filtration membrane 4.

If is possible fo have a two electrode system consisting of a working electrode 28 and a counter electrode 30.

When a diazonium salt is used fo build up a protective surface layer 40 fhe protective surface layer 40 is very resistant due to fhe nature of fhe covalenf bindings to fhe surface of fhe filtration membrane 4. The pro- tecfive surface layer 40 may be temperature resistant up to 300 degrees Celsius. Therefore, such protective surface layer 40 is useful fo filfer a huge area of fluids during rather extreme conditions. This includes liquid as well as gas separation af elevated temperatures. Fig. 5 a) is a close up view of a filtration layer 6 in a situation where no compounds 24 have been attached to fhe surface of fhe filtration layer 6. A group of diazonium salts 24 are present in fhe fluid near fhe filtration layer 6 of fhe filtration membrane 4. When free electrons, e-, are present (e.g. released from fhe electrically conducting filtration layer 6 of fhe filtration membrane 4) the diazonium salts 24 will react and decompose and release nitrogenous gas N2 and a radical, R, that can attach on the filtration layer 6 of fhe filtration membrane 4. A layer of attached compounds 26 constitute a protective surface layer 40 like fhe one indicated in Fig. 5 b).

Fig. 6 a) shows a close up view of a filtration layer 6 of a filtration membrane 4 according to fhe invention. The filtration membrane 4 is used to filfer a contaminated fluid. The fluid contains foulanfs 42, 43, 44. A protective surface layer 40 is attached on the filtration layer 6. The protec- five surface layer 40 prevenfs fhe foulanfs 42, 43, 44 from settling directly on fhe filtration layer 6. Instead fhe foulanfs 42, 43, 44 settle on the protective surface layer 40. Fig. 6 b) shows a close u p view of a filfrofion layer 6 of a filtration membrane 4 according fo fhe invenfion. Fig. 6 b) illustrates a situation where the protective surface layer 40 is being cleaved off fhe filtration layer 6 during a back flush process. If can be seen that the fouling layer fou- lanfs 42, 43, 44 are attached on the protective layer 40 of fhe filtration layer 6. The foulanfs 42, 44 and fhe main portion of fhe protective surface layer 40 are released from fhe filtration layer 6. In Fig. 6 b) a minor part of fhe protective surface layer 40 is still attached on the surface of fhe filtration layer 6 after the "cleave off process" has been carried out. The cleaved off process may be, af least partially, controlled by regulating the electrical potential at fhe working electrode 28 and/or fhe counter electrode 30 and/or the reference electrode 32. Fig. 7 a) illustrates a close up view of a grafted protective surface layer 40 where fhe compounds have long chains 38 so that the layer thickness L.2 of fhe protective surface layer 40 is relatively large. The grafted protective surface layer 40 may be a diazonium salt layer containing polyethylene glycol (PEG) chains. A multilayer 39 is grafted on the filfra- fion layer 6 by providing several layers on fhe top of each other. Hereby, a larger layer thickness L3 is achieved.

Fig. 7 b) illustrates a close up view of a grafted protective surface layer 40 where fhe compou nds have shorter chains 38. The layer thickness Li of fhe protective surface layer 40 is small com pared wifh the layer thickness Li illustrated in Fig. 7 a) .

Fig. 8 a) illustrates a graph showing the flux ratio 60 as function of time 62 for a typical filtration membrane that has not been modified and a filtration membrane according to fhe invention, respecfively. The flux ratio 60 as function of time 62 for fhe filtration membrane according to fhe present invenfion is indicated by fhe top curve 66. The flux ratio 60 as function of time 62 for the non-modified filtration membrane is indicated by the lower curve 68.

It can be seen that the flux ratio 60 of filtration membrane 4 according to the invention is higher than the flux ratio 60 of the prior art filtration membrane. It can also be seen that the flux ratio 60 of the prior art filtration membrane decreases much faster than the flux ratio 60 of the filtration membrane 4 according to the invention. The protective layer 40 on the filtration membrane 4 of the present invention inhibits growth of a fouling layer directly on the surface of the filtration layer 6 of the filtration membrane 4. Therefore, it is possible to keep the filtration layer of the filtration membrane 4 cleaner for a longer time period compared to a prior art filtration membrane. Since the filtration layer 6 of the filtration membrane 4 according to the invention is subject to less fouling or more easily removable fouling than a traditional non-modified filtration membrane, a high flux ratio 60 can be maintained over a long time period. This means that also the flux, under fixed pressure conditions, can be kept high. Fig. 8 b) is a graph showing the flux ratio 60 versus time 62 before and after a clean in place (CIP) process. The curve 68' is for a typical non- modified filtration membrane while curve 66' is for a filtration membrane 4 according to the invention. The CIP process is carried out at the same time 64 for both the prior art filtration membrane and the filtration membrane 4 according to the present invention. The CIP process is a process of cleaning the surface of the filtration layer 6 of the filtration membrane 4. It is possible to carry out the CIP process in a filtration system 2 without disassembling the filtration system 2. Often cleaning chemicals are used to achieve a sufficient cleaning of the surface. The CIP process is carried out in order to clean the filtration membrane so that the flux ratio is increased after a period of use where fouling and/or clogging have been induced. When the curves 66' and 68' are compared to one another it is noticeable that the filtration membrane 4 according to the invention is less sensitive to fouling than the non-modified filtration membrane. The pro- tective layer 40 attached on the surface of the filtration layer 6 of the filtration membrane 4 can explain this difference.

It is possible to make similar curves showing the transmembrane pressure (TMP) as function of time 62 instead of the flux ratio 60 versus time 62. In fact both the flux ratio 60 and the TMP indicate the filter capacity of the filtration membrane 4. When the flux ratio is close to 100% the filtration membrane is clean and suitable for being used to filter a fluid 14. When the flux ratio 60 is reduced the filter capacity of the filtration membrane 4 is also reduced. A low TMP indicates that the filtration membrane 4 is clean and thus that the filtration membrane 4 has a high filter capacity. A high TMP indicates that a fouling layer causes clogging of the filtration layer of the filtration membrane 4 and that the filtration membrane 4 needs to be cleaned. The limits imposed on when to initiate e.g. a back-flush or a CIP process depends on the specific filtration system and the fluid under investigation.

It can be seen from Fig. 8 b) that the flux ratio 60 is increased following the CIP process. This is indicated by the increasing curve portions 70 in Fig. 8 b).

Fig. 9 a) illustrates a number of diazonium salts 72, 74, 76, 78, 80 that may be used to build an anti fouling layer (a protective surface layer) on a filtration layer 6 of a filtration membrane 4 according to the invention.

The diazonium salt 72 is 4-(carboxyl) phenyl diazonium tetrafluoroborate which is easily synthesized using protocols well known to a person skilled in the art from the pertinent precursor (p-amino-benzoic acid). It may be advantageous to use this particular diazonium due to its hydrophilic character as well as its ability to be deprotonated/protonated as a function of pH, i.e. reversibly tune its hydrophilic character. This may be advantageous in media in which increasing the hydrophilic character of the membrane reduces the propensity of membrane fouling. It is also known that charged layers on membranes have a tendency to reduce fouling. The diazonium salt 74 is 4-(me†hoxy) phenyl diazonium tetrafluoroborate which is easily synthesized using protocols well known to a person skilled in the art from the pertinent precursor (p-me†hoxy aniline) Another highly related compound is provided by the commercially available Fast Blue BB salt. It may be advantageous to use these particular dia- zonium salts as they provide a simplified system incorporating the ether linkage between the benzene ring and substituent. This in part increases the hydrophilic character of the film and due to the electron donating nature of these substituents, these compounds are comparatively easy to oxidise (so that the protective surface layer can be cleaved off by way of example).

The diazonium salt 76 is 4-(2-(2-(me†hoxy)e†hoxy)e†hoxy) phenyl diazonium tetrafluoroborate which may offer significant advantages in that it incorporates an albeit short polyethylene glycol function in the layer. Such polyethylene glycol functionalities in membranes have by others been shown to make membranes much less prone to fouling. In particular it is known to reduce the so-called adsorptive fouling in which a first layer of water molecules is replaced by the fouling solute. This phenomenon is mainly due to its hydrophilic character. This may be advantageous in media in which increasing the hydrophilic character of the membrane reduces the propensity of membrane fouling. The forth example 78 is 4-(ni†ro) phenyl diazonium fefrafluoroborafe which is a well known diazonium salt†o a person skilled in the art. The advantage of this particular salt is that its hydrophilic character may be varied by controlling the oxidation state of the appended nitrogen atom. In the highest oxidation state, N02, it is marginally polar but can easily (by electrochemical means) be transformed into the reduced forms such as hydroxyl amine, -NHOH, or amine, -NH2. These latter will have pH activity and thus also have the option to exercise controlled hydrophilic character.

The final example, 80, is 4-(fluoro) phenyl diazonium tetrafluoroborate. The advantage of this particular species is that is introduces fluorinated functionalities on the surface on the membrane layer. This may increase the chemical resistance of the protective surface layer 40 as well as reduce the propensity of certain types of fouling to adsorb to the surface of the membrane.

As an additional embodiment, combinations of two or more diazonium salts to impose bi- and Afunctional layers on the surface may be ad- vantageous to reduce particular types of fouling on the surface.

Fig. 9 b) illustrates an example of a compound reaction causing deposition of an anti fouling layer (protective surface layer 40) on a filtration layer 6 of a filtration membrane 4 according to the invention. The cen- tral idea is that the diazonium salt 84 is electrochemically reduced in a one-electron process to release nitrogen gas 94 and the corresponding carbon centred radical. This radical 88 can then proceed according to a range of reaction mechanisms including homogeneous reactions, but most importantly also attach to the surface of the filtration layer 6. While the nature of the bond produced between the surface of the electrode and the layer has been the subject of some debate, there exists little doubt that the bonds 96 so made are strong and can persist even strong ultrasonic cleaning protocols.

Fig. 9 c) illustrates how additional layers of a compound 84' can be added to a compound 84 that is attached to the filtration layer 6 of a filtration membrane 4 like the one shown in Fig. 9 b) . The grafting process involving diazonium salts does not stop at the level indicated in Fig. 9 b). Rather the electrochemically generated radicals may react with groups already attached to the surface of the filtration layer 6. The de- gree to which this secondary process continues can to some extent be controlled by the applied electrochemical potential on the working electrode. The potential control exercised can have significant ramifications on the layer structure, density, and thickness. This will be known to a person skilled in the art.

List of reference numerals

2 - Filtration system

4 - Filtration membrane

6 - Filtration layer

8 - Porous base layer

1 0 - Pores

1 2 - Electrical source

1 4 - Fluid

1 6 - Fluid inlet

1 8 - Fluid outlet

20 - Permeate outlet

22 - Housing

24, 26 - Com pound

28 - Working electrode

30 - Counter electrode

32 - Reference electrode

34 - Seal ring (e.g. an O-ring

38 - End chain

40 - Protection layer

42, 43, 44 - Foulants

D, d - Layer thickness

Wi , W₂ - Width

X - Axis parallel to the surface of the filtration layer

Y - Axis perpendicular to the surface of the

filtration layer

46 - Base member

50 - Top member

52 - Cavity

54, 56, 58 - Wire

D, d, Li , L.2, L.3 - Layer thickness 60 Flux ratio

62 Time

64 Time for carrying out a CIP process

66, 66', 68, 68' Curve

70 Increasing curve portion

72 4-(carboxyl) phenyl diazonium

tetrafluoroborate

74 4-(me†hoxy) phenyl diazonium

tetrafluoroborate

76 4-(2-(2-(me†hoxy)e†hoxy)e†hoxy) phenyl diazonium

tetrafluoroborate

78 4-(ni†ro) phenyl diazonium tetrafluoroborate 80 is 4-(fluoro) phenyl diazonium tetrafluorobo- rate

84 Compound

86 Diazonium group

88 Aryl or alkyl

Benzene ring

92 Electron, e- 94 Nitrogenous gas (N2)

96 Covalent binding

Claims

A filtration membrane (4) comprising a porous base layer (8) attached to an electrically conductive filtration layer (6) having pores (10) extending through the filtration layer (6) characterised in that at least one compound (24, 26) is attached on the filtration layer (6) and hereby providing a protective surface layer (40) and that the at least one compound (24, 26) is configured to be at least partially cleaved off the filtration layer (6) by a predefined cleave off process.

A filtration membrane (4) according to claim 1 , characterised in that the at least one compound (24, 26) is configured to be attached on the filtration layer (6) and to be at least partially cleaved off the filtration layer (6) by a reversible electrochemical process.

A filtration membrane (4) according to claim 1 or claim 2 characterised in that the at least one compound (24, 26) is a dia- zonium salt: R-N2⁺ X^" , where R is aryl and where X is an inorganic or organic anion.

A filtration membrane (4) according to claim 1 or claim 2 characterised in that the at least one compound (24, 26) comprises one or more compounds configured to form a diazonium salt having the following form: R-N2⁺ X^" , where R is aryl and where X is an inorganic anion.

A filtration membrane (4) according to one of the preceding claims characterised in that the filtration membrane (4) is configured in a manner so that the thickness of the protective sur- face layers (40) can be controlled by using an electrochemical process.

A filtration membrane (4) according to one of fhe preceding claims characterised in that fhe diazonium compound is

A filtration membrane (4) according to one of fhe preceding claims characterised in that fhe filtration layer (6) is a metal layer.

If is also possible to have a filtration layer made in another electrically conductive material such as electrically conduction composite, carbon or another suitable material.

A filtration membrane (4) according to claim 6 characterised in that fhe filtration layer (6) is made of stainless steel.

If may be an advantage†o have a filtration membrane in which the porous base layer and fhe filtration layer are made of fhe same material.

If may beneficial fhe porous base layer and the filtration layer are made in stainless steel. A filtration membrane (4) according to one of the preceding claims characterised in that the pore size in the filtration layer (6) lies within the range between 5 nm and 500 nm, preferable between 10 nm and 200 nm.

10. A filtration membrane (4) according to one of the preceding claims characterised in that the pore size in the porous base layer (8) lies within the range between 100 nm to 100 μιτι, prefer- able 0,5-10 pm.

1 1 . A filtration membrane (4) according to one of the preceding claims characterised in that the thickness d of the filtration layer (6) is 50 nm-10 μιτι, preferable 200 nm-1000 nm.

12. A filtration membrane (4) according to one of the preceding claims characterised in that the thickness d of the porous base layer (8) is 300-3000 μιτι, preferable 500-1500 μηη. 13. A filtration system (2) comprising a filtration membrane (4) according to one of the preceding claims.

14. Method for filtration of a fluid (14) characterised in that a filter membrane (4) according to one of the claim 1 -12 is used to filter the fluid (14).